EP0102473A2 - Dispositif et procédé de purification sèche de gaz brulés - Google Patents
Dispositif et procédé de purification sèche de gaz brulés Download PDFInfo
- Publication number
- EP0102473A2 EP0102473A2 EP83106469A EP83106469A EP0102473A2 EP 0102473 A2 EP0102473 A2 EP 0102473A2 EP 83106469 A EP83106469 A EP 83106469A EP 83106469 A EP83106469 A EP 83106469A EP 0102473 A2 EP0102473 A2 EP 0102473A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluidized bed
- flue gas
- housing
- heat exchanger
- duct
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
Definitions
- the invention relates to a device for dry cleaning of flue gases contaminated with gaseous pollutants, in particular sulfur compounds, from the combustion of fossil fuels, primarily in boiler systems and furnaces, with a fluidized bed arranged in the flue gas duct from a fluidized bed containing absorbents above a floor grate and with a preheater for the combustion air and a cleaning process in the fluidized bed.
- gaseous pollutants in particular sulfur compounds
- a device of the type described at the beginning has become known (DE-OS 30 09 366), in which the flue gases are passed through a fluidized bed at a high temperature of approximately 700 to 900 degrees Celsius, which contains the absorbents, e.g. Contains calcium and / or magnesium compounds. Used absorbents are continuously withdrawn from the fluidized bed, which are replaced by fresh absorbents. The fluidized bed completely fills the cross section of the flue gas duct. The bottom grate of the fluidized bed is cooled. Air can be used as the coolant, which is then fed to the boiler as preheated combustion air. This facility is disadvantageous in several ways.
- the object of the invention is to improve the energy balance of a device of the type described at the outset, thus reducing the operating and investment costs and thereby achieving degrees of separation for the pollutants which are equivalent to those of wet processes and to work in a fluidized bed at an optimal operating temperature .
- This object is achieved in that a section of a regenerative heat exchanger which cools the flue gas is arranged in front of the fluidized bed in the flue gas duct, and a further section of the heat exchanger is connected into the combustion air duct, the Assignment of the common solid storage mass of the heat exchanger to its two sections changes continuously and periodically, and that a filter follows in the flue gas duct after the fluidized bed.
- the flue gases to be cleaned are passed through the cold section of the heat exchanger, as a result of which the flue gases are strongly cooled and the reaction temperature in the fluidized bed is low.
- the combustion air is heated up more, so that the boiler efficiency increases.
- new absorbents are always fed to the fluidized bed in accordance with its consumption.
- the fluidized bed itself can consist, for example, of a fine-grained quartz, grain size less than 2 mm. This is because the carrier material of the fluidized bed expediently consists of a sufficiently hard material which produces abrasion which can be removed from the absorbent material, so that there is constant activation. It may be advantageous to blow steam into the fluidized bed to improve the reactions.
- the flue gases leaving the fluidized bed are then freed of the entrained dust-like particles, primarily fine-grained reacted absorbents, in a filter.
- the filter forms a second reactive absorption layer, in which a subsequent separation of gaseous pollutant residues takes place.
- the fluidized bed with bottom grate and the regenerative heat exchanger are expediently arranged in a common housing, and a first sectoral (segment-like) section of the housing is connected on the inlet and outlet sides to the flue gas duct, while a second
- a device of the type described at the beginning has become known (DE-OS 30 09 366), in which the flue gases are passed through a fluidized bed at a high temperature of approximately 700 to 900 degrees Celsius, which contains the absorbents, for example calcium and / or contains magnesium compounds. Used absorbents are continuously withdrawn from the fluidized bed and are replaced by fresh absorbents. The fluidized bed completely fills the cross section of the flue gas duct.
- the bottom grate of the fluidized bed is cooled. Air can be used as the coolant, which is then fed to the boiler as preheated combustion air.
- This facility is disadvantageous in several respects. So that the flue gas can be discharged through a chimney as intended, the separation of the gaseous pollutants, in particular the sulfur compounds, must be carried out practically completely in the fluidized bed. However, this requires correspondingly long dwell times of the flue gas in the region of the fluidized bed with either a correspondingly low throughput or a high fluidized bed height with a considerable pressure loss of the flue gas.
- the high gas temperature causes large volume throughput rates. In order to avoid discharging the used absorbents with the flue gas, they must not be less than a minimum grain size.
- the object of the invention is to improve the energy balance of a device of the type described at the outset, thus reducing the operating and investment costs and thereby achieving degrees of separation for the pollutants which are equivalent to those of wet processes and to work in a fluidized bed at an optimal operating temperature .
- This object is achieved in that a section of a regenerative heat exchanger which cools the flue gas is arranged in front of the fluidized bed in the flue gas duct, and a further section of the heat exchanger is connected into the combustion air duct, the vice versa.
- cleaning devices that are optimized for the respective application can be implemented, which largely return the flue gas heat to the combustion air with appropriate outlay in terms of equipment, with high degrees of separation of the pollutants, and thus considerably improve the overall energy balance of the furnace or boiler system.
- the fluidized bed can be designed in such a way that it has separate separating layers for S0 2 , SO 3 , C1 and F on the one hand and NO x on the other.
- the various deposition layers are expediently arranged one above the other.
- a dust filter with a high degree of separation in the flue gas duct in front of the fluidized bed, in which the solid particles carried by the flue gas are separated.
- the solid particles carried by the flue gas are separated.
- the material extracted from the filter consists largely of gypsum.
- a customary aftertreatment can be carried out, for example by washing out the calcium chloride and oxidizing the sulfite to calcium sulfate.
- This ensures a high degree of separation and prevents acid separation in subsequent parts of the system sectorial (segment-like) section of the housing is connected into the combustion air channel and the regenerative storage mass body is arranged below the fluidized bed.
- the fluidized bed with a bottom grate is designed to be stationary in the housing, while the regenerative storage mass body of the heat exchanger rotates about a coaxial axis.
- the storage mass body of the heat exchanger preferably consists of laminated cores arranged radially at a distance in the circumferential direction, so that flue gas and combustion air flow vertically in this area.
- the cleaning device contains flue-containing flue gas that has not been adequately filtered beforehand, it is advisable to equip the housing with a third, approximately sectoral section for cleaning air conducted in the X-cycle, so that no dusts are carried into the combustion air.
- a regenerative heat exchanger 8 which is circular in horizontal cross section, is arranged in the fixed housing 7 in the lower region and is designed to rotate about the shaft 10 via the drive 9.
- the known heat exchanger consists of vertical laminated cores 11 arranged radially in the circumferential direction at a distance (FIG. 3).
- the housing 7, which is circular in cross section at the bottom, is divided by two inner partition walls 12 into two segment-like sections 13, 14, each of which continues upwards like a tower. 6 schematically illustrates the fixed housing segments 13 and 14 of the cross section along the line VI-VI in FIG. 2.
- a fluidized bed 16 is arranged above the floor grate 15 , which is loaded with absorbent via the lance 17.
- the treated flue gas is passed on via the flue gas duct section 18.
- the second segment-like section 14 of the housing 7 is connected to the duct sections 19, 20 for combustion air.
- the combustion air is warmed up there by the hot laminated cores 11 releasing their heat content to the combustion air.
- the fluidized bed 16 is operated by the flue gas. It consists of fine-grained quartz with a grain size of less than 2 mm and an absorbent in fine form, preferably with a commercially available grain size of less than about 200p, from one or more calcium compounds. These compounds react with gaseous pollutants carried by the flue gases, such as S0 2 , Cl, F and the like.
- the basic mass of the fluidized bed consisting of "quartz" is much harder than the absorbents, so that the latter become increasingly fine-grained during operation as a result of grinding and therefore remain highly reactive for a very long time, the abrasion and ultimately the residual grain being discharged with the flue gas.
- rotatable flaps 21 are arranged between the fluidized bed 16 and the heat exchanger 8, which in the blocking position allow the average cross section for the flue gas to be reduced in an appropriate gradation in order to adapt to variable flue gas flow rates.
- the suction line 40 leads flue gas reaching between the partitions 12 back under the fluidized bed 16.
- the flue gas from a boiler 1 via a flue gas channel 2 first into a dust separator 3, from which the accumulating dust is discharged in a known manner in the direction of arrow 4.
- the dust separator 3 can be, for example, a centrifugal separator or can be designed as a hot gas filter with a high degree of separation for flue gas dust.
- a flue gas duct section 5 adjoins the dust separator 3 and ends under a device 6 for dry flue gas cleaning, which is accommodated in a common housing 7.
- FIG. 6 shows schematically the division of the housing 7 into a fixed flue gas segment 13 and a fixed combustion air segment 14, in contrast to which the regenerative storage mass body 8 and the fluidized bed 16 with bottom grate 15 are continuously rotating.
- the device 6 has yet another air duct in which cleaning air is circulated.
- the fixed housing 7 has three sectoral or segment-like sections, as is shown schematically in FIG. 7.
- a smaller sector 34 adjoins the flue gas segment 13 and occupies approximately 1/8 of the circular area.
- the device 6 is connected to duct sections for hot cleaning air, not shown above and below, so that the dust particles deposited in the fluidized bed and on the floor grate are discharged and not get into the combustion air.
- the dust separator 3 FIG. 1
- the device 6 corresponds to the essential components of the embodiment according to FIGS. 2 or 4.
- the cleaning device 6 is shown in an embodiment with a fixed in the stationary housing 7 fluidized bed 16 with bottom grate 15 and fixed heat exchanger 8, which are circular or circular in cross-section and are arranged coaxially one above the other.
- a double-winged rotating hood 35 is formed in the interior of the housing 7, rotating synchronously by means of shaft 10 and drive 9.
- the combustion air is guided between the central duct sections 36, 37 via the two hoods 35.
- the fluidized bed 16 is located exclusively in the flue gas duct with an advantageously large flow cross section.
- Fig. 9 shows schematically At the top of the device 6, a flue gas channel section 1 8 includes (Fig.
- a filter 2 2 which may be for example a fabric filter or an electrostatic precipitator.
- the fine-grained particles carried by the flue gases essentially contain the fully absorbed absorbent. They settle on the filter fabric and form a further absorption layer consisting primarily of calcium sulfate and calcium sulfite.
- the cleaned flue gases pass into the chimney 24 via a suction draft 23.
- the sulfate / sulfite mixture discharged from the filter 22 can be used in the present form, for example as an additive to cement, and is discharged for this purpose on the trigger 41.
- a return line 42 enables repeated treatment in the fluidized bed 16 if necessary.
- a customary post-treatment of the material can be carried out.
- it is fed to a container 25 with agitator 26 and mixed there with water. If necessary, such consumed absorbents which are not discharged from the fluidized bed 16 are also transferred into the container 25 (line 29).
- the mixture is conveyed from the container 25 into an oxidation container 28 by means of a pump 27, which is supplied with sulfuric acid at 43 and which is flushed with air supplied from below at 44.
- the flue gas is connected via the channel sections 5, 18 and the combustion air via the channel sections 19, 20 to the fixed housing 7, which is divided into two segment-like sections 13 by the two inner partition walls 12, 14 (Fig. 5) is divided.
- the fluidized bed 16 with bottom grate 15 and the regenerative storage mass body 8 are circular in cross section, arranged coaxially one above the other and firmly connected to one another via the rotatably mounted shaft 10; they are rotated by the drive 9.
- the flue gas flows in its housing segment 13 from the heat Separate liquid sulfuric acid, which together with the existing dust and chlorine gas are highly aggressive. The large transfer of thermal energy from the flue gas into the combustion air makes the operation of the boiler 1 more economical.
- Gypsum with high foreign body purity is obtained in the embodiments which - as already mentioned - have a hot gas filter as dust separator 3. If the separator 3 is e.g. a centrifugal separator, then fine dust particles get into the filter 22 and are also processed in the system parts 25 - 32, so that no clean gypsum is produced, but a usable, inexpensive hydraulically setting construction material is nevertheless obtained.
- the separator 3 is e.g. a centrifugal separator, then fine dust particles get into the filter 22 and are also processed in the system parts 25 - 32, so that no clean gypsum is produced, but a usable, inexpensive hydraulically setting construction material is nevertheless obtained.
- the sulfur content of the flue gas is excreted as a solid in the fluidized bed.
- the fabric filter there is usually a degree of separation of over 85%, so that wet cleaning systems are no longer superior.
- the product withdrawn from the filter 22 consists largely of calcium sulfate with calcium sulfite and chloride components, which are often no longer disruptive, so that a washing and oxidizing aftertreatment may also be omitted.
- the flue gas outlet temperature at the fluidized bed 16 can be very low, namely below 120 ° C and possibly reduced to about 80 ° C. Given the high degree of separation achieved, the sulfuric acid dew point (approx. 120 ° C) becomes uncritical, so that only the water dew point (40 ° - 50 ° C) has to be observed.
- the flue gas inlet temperature at the fluidized bed 16 can be, for example, approximately 160 ° C. The measure of placing the acid dew point in the fluidized bed achieves a liquid phase of the sulfurous acid on the grain surfaces of the fluidized bed, thus creating excellent conditions for SO 2 absorption.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Meat, Egg Or Seafood Products (AREA)
- Chimneys And Flues (AREA)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT83106469T ATE24121T1 (de) | 1982-07-23 | 1983-07-02 | Einrichtung und verfahren zur trockenen rauchgasreinigung. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3227553 | 1982-07-23 | ||
| DE3227553A DE3227553C2 (de) | 1982-07-23 | 1982-07-23 | Vorrichtung zur trockenen Rauchgasreinigung |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| EP0102473A2 true EP0102473A2 (fr) | 1984-03-14 |
| EP0102473A3 EP0102473A3 (en) | 1984-04-11 |
| EP0102473B1 EP0102473B1 (fr) | 1986-12-10 |
Family
ID=6169150
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP83106469A Expired EP0102473B1 (fr) | 1982-07-23 | 1983-07-02 | Dispositif et procédé de purification sèche de gaz brulés |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0102473B1 (fr) |
| JP (1) | JPS5932923A (fr) |
| AT (1) | ATE24121T1 (fr) |
| DE (2) | DE3227553C2 (fr) |
| DK (1) | DK332783A (fr) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0226731A1 (fr) * | 1985-10-22 | 1987-07-01 | Apparatebau Rothemühle Brandt & Kritzler Gesellschaft mit beschränkter Haftung | Dispositif pour diminuer l'émission de la matière nocive dans les gaz d'échappement des installations de combustion |
| EP0718476A1 (fr) * | 1994-12-21 | 1996-06-26 | Toyota Jidosha Kabushiki Kaisha | Dispositif d'épuration de gaz d'éschappement |
| CN117968250A (zh) * | 2024-03-22 | 2024-05-03 | 山东中汇能新能源科技有限公司 | 固体蓄热式电锅炉 |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB708369A (en) * | 1950-12-28 | 1954-05-05 | Svenska Rotor Maskiner Ab | Improvements in rotary regenerative air preheaters or like rotary drum apparatus |
| US3780498A (en) * | 1972-03-31 | 1973-12-25 | Universal Oil Prod Co | Sulfur oxides removal system |
| US4236464A (en) * | 1978-03-06 | 1980-12-02 | Aerojet-General Corporation | Incineration of noxious materials |
| DE2931546A1 (de) * | 1979-08-03 | 1981-02-26 | Heinz Ing Grad Hoelter | Verfahren und vorrichtung zur trockenen chemisorption hinter wirbelbettkohlefeuerungsanlagen zur abscheidung von so tief 2 , no tief x , hcl und hf aus rauchgasen |
| DE2942126C2 (de) * | 1979-10-18 | 1982-10-14 | L. & C. Steinmüller GmbH, 5270 Gummersbach | Wärmeleitelemente für regenerativen Wärmeaustausch |
| DE3009366A1 (de) * | 1980-03-12 | 1981-09-24 | Wehrle-Werk Ag, 7830 Emmendingen | Einrichtung zur trocknen entfernung von schadstoffen aus rauchgasen |
| DE3035386C2 (de) * | 1980-09-19 | 1985-08-29 | Apparatebau Rothemühle Brandt + Kritzler GmbH, 5963 Wenden | Anwendung von als Hohlkugeln oder als hohle Vielflächner ausgebildeten, wärmeübertragenden Elementen in einem regenerativen Wärmetauscher |
-
1982
- 1982-07-23 DE DE3227553A patent/DE3227553C2/de not_active Expired
-
1983
- 1983-07-02 AT AT83106469T patent/ATE24121T1/de not_active IP Right Cessation
- 1983-07-02 DE DE8383106469T patent/DE3368204D1/de not_active Expired
- 1983-07-02 EP EP83106469A patent/EP0102473B1/fr not_active Expired
- 1983-07-19 DK DK332783A patent/DK332783A/da not_active Application Discontinuation
- 1983-07-22 JP JP58133021A patent/JPS5932923A/ja active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0226731A1 (fr) * | 1985-10-22 | 1987-07-01 | Apparatebau Rothemühle Brandt & Kritzler Gesellschaft mit beschränkter Haftung | Dispositif pour diminuer l'émission de la matière nocive dans les gaz d'échappement des installations de combustion |
| EP0718476A1 (fr) * | 1994-12-21 | 1996-06-26 | Toyota Jidosha Kabushiki Kaisha | Dispositif d'épuration de gaz d'éschappement |
| US5697211A (en) * | 1994-12-21 | 1997-12-16 | Toyota Jidosha Kabushiki Kaisha | Exhaust gas purification device |
| CN117968250A (zh) * | 2024-03-22 | 2024-05-03 | 山东中汇能新能源科技有限公司 | 固体蓄热式电锅炉 |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0102473B1 (fr) | 1986-12-10 |
| DK332783D0 (da) | 1983-07-19 |
| DE3368204D1 (en) | 1987-01-22 |
| ATE24121T1 (de) | 1986-12-15 |
| DE3227553A1 (de) | 1984-01-26 |
| JPS5932923A (ja) | 1984-02-22 |
| DK332783A (da) | 1984-01-24 |
| DE3227553C2 (de) | 1986-04-24 |
| EP0102473A3 (en) | 1984-04-11 |
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